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WO2024181909A1 - Séparateur de particules, système comprenant un tel séparateur de particules, et procédés de calcination - Google Patents

Séparateur de particules, système comprenant un tel séparateur de particules, et procédés de calcination Download PDF

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Publication number
WO2024181909A1
WO2024181909A1 PCT/SE2024/050193 SE2024050193W WO2024181909A1 WO 2024181909 A1 WO2024181909 A1 WO 2024181909A1 SE 2024050193 W SE2024050193 W SE 2024050193W WO 2024181909 A1 WO2024181909 A1 WO 2024181909A1
Authority
WO
WIPO (PCT)
Prior art keywords
calcination
gas
particle separator
input material
process products
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
PCT/SE2024/050193
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English (en)
Inventor
Roland LUNDKVIST
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Limearc Process AB
Original Assignee
Limearc Process AB
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from SE2350232A external-priority patent/SE545972C2/en
Priority claimed from SE2350231A external-priority patent/SE547412C2/en
Application filed by Limearc Process AB filed Critical Limearc Process AB
Publication of WO2024181909A1 publication Critical patent/WO2024181909A1/fr
Anticipated expiration legal-status Critical
Pending legal-status Critical Current

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Classifications

    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters
    • D21C11/12—Combustion of pulp liquors
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J19/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J19/24—Stationary reactors without moving elements inside
    • B01J19/2405—Stationary reactors without moving elements inside provoking a turbulent flow of the reactants, such as in cyclones, or having a high Reynolds-number
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J4/00—Feed or outlet devices; Feed or outlet control devices
    • B01J4/001—Feed or outlet devices as such, e.g. feeding tubes
    • B01J4/002—Nozzle-type elements
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J6/00—Heat treatments such as Calcining; Fusing ; Pyrolysis
    • B01J6/001—Calcining
    • C—CHEMISTRY; METALLURGY
    • C04—CEMENTS; CONCRETE; ARTIFICIAL STONE; CERAMICS; REFRACTORIES
    • C04B—LIME, MAGNESIA; SLAG; CEMENTS; COMPOSITIONS THEREOF, e.g. MORTARS, CONCRETE OR LIKE BUILDING MATERIALS; ARTIFICIAL STONE; CERAMICS; REFRACTORIES; TREATMENT OF NATURAL STONE
    • C04B2/00—Lime, magnesia or dolomite
    • C04B2/10—Preheating, burning calcining or cooling
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters
    • D—TEXTILES; PAPER
    • D21—PAPER-MAKING; PRODUCTION OF CELLULOSE
    • D21C—PRODUCTION OF CELLULOSE BY REMOVING NON-CELLULOSE SUBSTANCES FROM CELLULOSE-CONTAINING MATERIALS; REGENERATION OF PULPING LIQUORS; APPARATUS THEREFOR
    • D21C11/00—Regeneration of pulp liquors or effluent waste waters
    • D21C11/04—Regeneration of pulp liquors or effluent waste waters of alkali lye
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00121—Controlling the temperature by direct heating or cooling
    • B01J2219/00123—Controlling the temperature by direct heating or cooling adding a temperature modifying medium to the reactants
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/00049—Controlling or regulating processes
    • B01J2219/00051—Controlling the temperature
    • B01J2219/00159—Controlling the temperature controlling multiple zones along the direction of flow, e.g. pre-heating and after-cooling
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J2219/0873—Materials to be treated
    • B01J2219/0877—Liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J2219/00—Chemical, physical or physico-chemical processes in general; Their relevant apparatus
    • B01J2219/08—Processes employing the direct application of electric or wave energy, or particle radiation; Apparatus therefor
    • B01J2219/0894—Processes carried out in the presence of a plasma
    • B01J2219/0898—Hot plasma

Definitions

  • Embodiments herein relate to a particle separator to be used in systems for thermal treatment of solid chemical compounds. Further embodiments herein relate in general to systems, apparatus and methods for thermal treatment of solid chemical compounds.
  • the system comprises a particle separator arranged to receive input material in the form of particles.
  • a particle separator is provided.
  • the particle separator is arranged to receive input material.
  • the particle separator comprises a chamber configured to hold a fluid bed of particles mixed with gas, into which fluid bed gas is fluing from underneath, thereby separating smaller particles from larger particles by lifting the smaller particles upwards in the flow of gas.
  • the particle separator is coupled to a transfer channel arranged to provide the flow of the separated smaller particles mixed with gas to an injection arrangement injecting the provided input material into the heated calcination reactor.
  • a calcination system comprising a heated calcination reactor.
  • the heated reactor is configured to convert input material into calcination process products comprising a solid compound and a gas.
  • the system comprises a particle separator arranged to receive input material.
  • the particle separator comprises a chamber configured to hold a fluid bed of particles mixed with gas, into which fluid bed gas is fluing from underneath, thereby separating smaller particles from larger particles by lifting the smaller particles upwards in the flow of gas.
  • the particle separator is coupled to a transfer channel arranged to provide the flow of the separated smaller particles mixed with gas to an injection arrangement injecting the provided input material into the electrically heated calcination reactor.
  • the particle separator may further be arranged to communicate with a control unit communicatively coupled to sensors and control actuators and configured to receive sensor signals, to generate control signals and to communicate control signals through a control port connected to one or more signal lines coupled to the sensors and control actuators.
  • the control unit may be configured to control one or more of heated gas flow from above into the particle separator, and gas flow from underneath into the fluid bed.
  • the particle separator may further comprise a trapdoor device arranged to release larger particles separated from the fluid bed.
  • the particle separator may further be further comprise a valve arranged to regulate the gas flow from underneath to the fluid bed.
  • the particle separator may further comprise a flow regulator regulating the flow of gas through the valve.
  • the flow regulator may be arranged to control the flow of gas through the valve by use of any of the following parameters, the flow of gas supplied to the fluid bed, a first pressure measured inside the chamber, a second pressure measured outside the chamber, and the difference between the first and the second pressure, and if the calculated difference is negative, increasing the gas supply, and if the calculated difference is positive, decreasing the gas supply whereby a pressure balance is achieved.
  • the calcination system may further comprise an input material preheater coupled to an input and configured to conduct input material to the particle separator in a plurality of channels.
  • a calcination system may further comprise a first heat recovery arrangement configured to receive the calcination process products, to extract heat from the calcination process products and transfer the extracted heat to the input material in the input material preheater.
  • the calcination system may further comprise a second heat recovery arrangement configured to extract heat from solid compound in the form of calcium oxide of the calcination process products output from the electrically heated calcination reactor and separated from the gas in the form of carbon dioxide of the calcination process products. The extracted heat is carried by a gas and inserted into the injection arrangement.
  • the calcination system may further comprise a first separator configured to receive calcination process products from the electrically heated calcination reactor and to separate solid compound in the form of calcium oxide from the gas in the form of carbon dioxide of the calcination process products.
  • the calcination system may further comprise a second separator configured to receive residual calcination process products output from the first separator and from the first heat recovery system. The second separator is configured to further separate solid compound in the form of calcium oxide from the gas in the form of carbon dioxide of the residual calcination process products.
  • the calcination system may further comprise a control unit communicatively coupled to sensors and control actuators, and configured to receive sensor signals, to generate control signals and to communicate control signals through a control port connected to one or more signal lines coupled to the sensors and control actuators.
  • the control unit may be configured to control one or more of driving gas supply into the input material preheater, injection gas supply into the injection arrangement, heated gas in the particle separator, gas pressure in the calcination chamber and/or temperature in the calcination chamber and gas supply into the particle separator to support the fluid bed.
  • a method comprises separating, in a particle separator, smaller particles from larger particles of solid compound in input material, and conveying the smaller particles in a gas flow to an injection arrangement for injection into an electrically heated calcination reactor.
  • the method may further comprise controlling the gas supply into the particle separator to support the fluid bed comprises by one or more of, measuring the supplied gas flow, measuring a first pressure inside the chamber, measuring a second pressure outside the chamber, calculating the difference between the first and the second pressure, and if the calculated difference is negative, increasing the gas supply, and if the calculated difference is positive, decreasing the gas supply whereby a pressure balance is achieved.
  • a calcination method comprises receiving input material in the form of lime mud, separating smaller particles from larger particles of input material in a fluid bed by lifting the smaller particles upwards in a flow of gas, providing the flow of the separated smaller particles mixed with gas to an injection arrangement, injecting the separated input material into an electrically heated calcination reactor by use of the injection arrangement, converting, in the electrically heated calcination reactor input material into calcination process products comprising a solid compound in the form of calcium oxide and a gas in the form of carbon dioxide, extracting, in a first heat recovery arrangement heat from the calcination process products and transferring the extracted heat to the input material in the input material preheater, and separating, in one or more separators, the solid compound in the form of calcium oxide and gas in the form of carbon dioxide of the calcination process products.
  • the calcination method may further comprise extracting, in a second heat recovery arrangement, heat from solid compound in the form of calcium oxide of the calcination process products output from the electrically heated calcination reactor and separated from the gas in the form of carbon dioxide of the calcination process products, carrying the extracted heat by a gas and inserting the heat carrying gas into the injection arrangement.
  • the calcination method may further comprise separating, in a first separator, calcination process products received from the electrically heated calcination reactor such that solid compound in the form of calcium oxide is separated from the gas in the form of carbon dioxide of the calcination process products. Still further, in embodiments herein the calcination method may further comprise separating, in a second separator, residual calcination process products received from the first separator and from the first heat recovery system such that further solid compound in the form of calcium oxide is separated from the gas in the form of carbon dioxide of the residual calcination process products.
  • the calcination method may further comprise receiving sensor signals, generating control signals, and communicating control signals through a control port (128) connected to one or more signal lines (130) coupled to said sensors and control actuators, by use of a control unit (126) communicatively coupled to sensors, actuators and other control means.
  • the calcination method may further comprise controlling one or more of driving gas supply into the input material preheater, injection gas supply into the injection arrangement, heated gas in the particle separator, gas pressure in the calcination chamber and/or temperature in the calcination chamber, and gas supply into the particle separator to support the fluid bed.
  • controlling the gas supply into the particle separator to support the fluid bed may comprises one or more of measuring the supplied gas flow, measuring a first pressure inside the particle separator, measuring a second pressure outside the particle separator calculating the difference between the first and the second pressure, and if the calculated difference is negative, increasing the gas supply, and if the calculated difference is positive, decreasing the gas supply whereby a pressure balance is achieved.
  • a calcination method comprises receiving input material in the form of lime mud, separating smaller particles from larger particles of input material in a fluid bed by lifting the smaller particles upwards in a flow of gas, providing the flow of the separated smaller particles mixed with gas to an injection arrangement, injecting the separated input material into an electrically heated calcination reactor by use of the injection arrangement, converting, in the electrically heated calcination reactor input material into calcination process products comprising a solid compound in the form of calcium oxide and a gas in the form of carbon dioxide, extracting, in a first heat recovery arrangement heat from the calcination process products and transferring the extracted heat to the input material in the input material preheater, and separating, in one or more separators, the solid compound in the form of calcium oxide and gas in the form of carbon dioxide of the calcination process products.
  • the calcination method may further comprise extracting, in a second heat recovery arrangement, heat from solid compound in the form of calcium oxide of the calcination process products output from the electrically heated calcination reactor and separated from the gas in the form of carbon dioxide of the calcination process products, carrying the extracted heat by a gas and inserting the heat carrying gas into the injection arrangement.
  • the calcination method may further comprise separating, in a first separator, calcination process products received from the electrically heated calcination reactor such that solid compound in the form of calcium oxide is separated from the gas in the form of carbon dioxide of the calcination process products. Still further, in embodiments herein the calcination method may further comprise separating, in a second separator, residual calcination process products received from the first separator and from the first heat recovery system such that further solid compound in the form of calcium oxide is separated from the gas in the form of carbon dioxide of the residual calcination process products.
  • the calcination method may further comprise receiving sensor signals, generating control signals, and communicating control signals through a control port (128) connected to one or more signal lines (130) coupled to said sensors and control actuators, by use of a control unit (126) communicatively coupled to sensors, actuators and other control means.
  • the calcination method may further comprise controlling one or more of driving gas supply into the input material preheater, injection gas supply into the injection arrangement, heated gas in the particle separator, gas pressure in the calcination chamber and/or temperature in the calcination chamber, and gas supply into the particle separator to support the fluid bed.
  • controlling the gas supply into the particle separator to support the fluid bed may comprises one or more of measuring the supplied gas flow, measuring a first pressure inside the particle separator, measuring a second pressure outside the particle separator calculating the difference between the first and the second pressure, and if the calculated difference is negative, increasing the gas supply, and if the calculated difference is positive, decreasing the gas supply whereby a pressure balance is achieved.
  • FIG 1 shows a schematic overview of one example of a calcination system comprising a particle separator in accordance with embodiments herein.
  • FIG 2 shows an exemplified embodiment of a particle separator.
  • FIG 1 show one example of a system 100 configured for carrying out embodiments of methods herein, here exemplified by an adaptation to calcination of lime mud, for example applicable in a lime recovery cycle in cellulose industry.
  • embodiments are generally useable and/or configurable thermal treatment of other input materials.
  • FIG 1 also serves as a schematic flow chart for embodiments of calcination methods.
  • any embodiment of systems, injection arrangements, particle separators or any other arrangements disclosed herein, as well as any methods, may be applied independently or in any combination with any other embodiments described herein.
  • any embodiments described in this disclosure may be applied independently or in combination with other embodiments described herein. It may further be noted that any heated reactor may be employed.
  • Thermal treatment of a solid chemical compound is commonly called calcination.
  • the compound is heated to high temperature below the melting point of the solid chemical compound generally under restricted supply of ambient oxygen.
  • the general purpose may be to achieve thermal decomposition and/or to remove impurities or volatile substances.
  • Calcination of lime is for example applicable in lime recovery cycles in process industry such as in the cellulose industry, in the cement industry or in the metal industry.
  • lime comprising crystal forms of calcium carbonate (CaCO3) is thermally decomposed to calcium oxide (CaO), also called quick lime, and carbon dioxide (CO2).
  • CaCO3 also called quick lime
  • CO2 carbon dioxide
  • the calcination reaction is CaCO3(s) —> CaO(s) + CO2(g), where (s) denotes solid compound and (g) denotes gas form compound.
  • lime mud is a by-product obtained in pulp mills as part of the process that turns wood into pulp for paper.
  • wood chips are cooked with sodium hydroxide to extract the wood fiber used to make paper from the lignin that binds the wood together.
  • sodium hydroxide is converted to sodium carbonate.
  • Calcium oxide also known as quicklime, is then added to convert the sodium carbonate back to sodium hydroxide in order to use it again.
  • calcium carbonate in the form of lime mud is obtained.
  • Lime mud is mainly calcium carbonate mixed with water forming a sludge. The lime mud is then calcined to retrieve calcium oxide in a lime recovery cycle.
  • the lime mud is preferably dried to an extent suitable for handling in connection with and in the calcination process.
  • the input material such as lime or lime mud may be pulverized into a powder in connection with the drying. Similar processes are as mentioned applicable in other industries.
  • Calcination of calcium carbonate begins to occur at about 900 degrees Celsius, and normally calcination takes place at temperatures in the range 900-1100 degrees Celsius, whereby calcium oxide and carbon dioxide is formed.
  • the calcination reaction is reversible, and in order to avoid reformulation of calcium carbonate in the presence of carbon dioxide the temperature must be maintained above the calcination temperature.
  • temperature raising to about 1100 degrees Celsius and above the calcium oxide sinters With temperature raising to about 1100 degrees Celsius and above the calcium oxide sinters. In the sintering process the calcium oxide is compacting in the phenomenon that calcium crystals are collapsed and forming a solid mass of material. The rate of the sintering is increased with higher temperature.
  • water vapor herein also called steam
  • the process should be kept free from water vapor.
  • carbon dioxide CO2 is released from the calcium carbonate and after sintering the calcium oxide is more stable.
  • the quick lime is usually slaked with green liquor.
  • FIG 1 an example of a calcination system 100 comprising a particle separator 110 is shown.
  • the system 100 comprises an input 102 for material to be thermally treated, for example an input in the form of a lime mud storage container.
  • the exemplified calcination system comprise an input 102 for receiving input material, for example in the form of lime mud.
  • Input material may be in the form of lime raw material, which herein is material comprising calcium carbonate containing minerals or substances such as limestone, lime sludge, dolomite, calcium containing sludge.
  • the particle separator 110 may be used in any calcination system.
  • the particle separator 110 is arranged to receive input material in the form of particles of lime mud.
  • the particles are supplied at the top of the particle separator 110.
  • the supplied particles may be supplied mixed with gas, and they may be preheated before supplied to the particle separator 110.
  • the particle separator 110 comprises a chamber 401 configured to hold a fluid bed 402 of particles mixed with gas, into which fluid bed 402 gas is fluing from underneath 403, thereby separating smaller particles from larger particles by lifting the smaller particles upwards in the flow of gas.
  • the separated larger particles will due to gravity forces move downwards in the particle separator 110.
  • the particle separator 110 is coupled to a transfer channel 404 arranged to provide the flow of the separated smaller particles mixed with gas to an injection arrangement injecting the provided input material into an electrically heated calcination reactor 108.
  • the fluid bed 402 is controlled by the gas provided from underneath 403. As shown in FIG 2, the gas is supplied via a valve and a flow control unit. A first pressure is measured inside the chamber 401 by use of a first pressure sensor, and a second pressure is measured outside the chamber 401 by use of a second pressure sensor. The difference of the first and second pressure is calculated and may be used to control the flow in the valve providing gas to the fluid bed 402.
  • the particle separator 110 is configured to separate larger and heavier lumps of preheated material, such as lime mud, from smaller and lighter particles of material.
  • the particle separator 110 is arranged such that lumps of material by gravity falls into a lump collection container and such that smaller particles are lifted by a stream of pre-heated gas and input into the injector arrangement 106.
  • the particle separator 110 is provided with a controllable supply of heated gas.
  • the supply of heated gas may be controllable by one or more actuators, preferably coupled to a control unit 126.
  • the particle separator 110 may be coupled to an injection arrangement 106 and configured to convey smaller particles in a gas flow to the injection arrangement 106 for injection into the electrically heated calcination reactor 108.
  • a calcination system 100 comprising an electrically heated calcination 108 reactor.
  • the electrically heated calcination reactor 108 is configured to convert input material into calcination process products comprising a solid compound in the form of calcium oxide and a gas in the form of carbon dioxide.
  • the system 100 further comprises a particle separator 110 arranged to receive input material in the form of particles of lime mud.
  • the particle separator 110 comprises a chamber 401 configured to hold a fluid bed 402 of particles mixed with gas, into which fluid bed 402 gas is fluing from underneath 403, thereby separating smaller particles from larger particles by lifting the smaller particles upwards in the flow of gas.
  • the particle separator is coupled to a transfer channel 404 arranged to provide the flow of the separated smaller particles mixed with gas to an injection arrangement injecting the provided input material into the electrically heated calcination reactor 108.
  • Methods herein may comprise receiving sensor signals, generating control signals, and communicating control signals through a control port 128 connected to one or more signal lines 130 coupled to the sensors and control actuators, by use of a control unit 126 communicatively coupled to sensors, actuators and other control means. Methods herein may further comprise controlling one or more of heated gas in the particle separator, and gas supply into the particle separator to support the fluid bed.
  • Controlling the gas supply into the particle separator to support the fluid bed may comprise one or more of measuring the supplied gas flow, measuring a first pressure inside the particle separator, measuring a second pressure outside the particle separator and calculating the difference between the first and the second pressure, and, if the calculated difference is negative, increasing the gas supply, and if the calculated difference is positive, decreasing the gas supply whereby a pressure balance is achieved.
  • Methods herein comprises separating, in a particle separator 110 coupled to the injection arrangement 106, such that larger lumps and smaller particles of solid compound in input material are separated, and conveying the smaller particles in a gas flow to the injection arrangement 106 for injection into the electrically heated calcination reactor 108.
  • the particle separator 110 may be configured or controlled such that particles of pre-heated input material with a size in the range of 1 to 1000 micrometers are input to the calcination reactor 108 via the injection arrangement 106. With powder form the contact surface of the input material will become very large, whereby the contact time with heat in the calcination reactor can be minimized.
  • the calcination reactor is in the exemplifying figures shown as a plasma reactor, but the input material preheater may be used together with any type of calcination reactor.
  • the injection arrangement 106 is configured to convey and inject the input material, for example heated lime mud, into an electrically heated calcination reactor 108.
  • the injection arrangement is coupled to a particle separator 110.
  • Embodiments of the calcination system 100 comprises an injection arrangement 106 configured to receive input material from the input material preheater 104 and to inject input material into an electrically heated calcination reactor 108.
  • Embodiments of a calcination method comprises injecting input material into an electrically heated calcination reactor 108.
  • Embodiments of the injection arrangement 106 comprises an inlet for an injection gas supply 107 configured to enable feeding of an injection gas at a controllable pressure, for example in the range of 1-5 ata (atmospheric pressure above vacuum).
  • the purpose of the injection gas is to control the injection rate, the injection pressure, the distribution and/or the temperature of the pre-heated input material injected into the electrically heated calcination reactor 108.
  • the inlet for injection gas supply is controllable by one or more actuators, preferably coupled to control unit 126.
  • the injection gas is carbon dioxide CO2 or steam.
  • the injection gas is in embodiments recycled carbon dioxide CO2 recovered from the calcination process.
  • Embodiments of an injection arrangement 106 in a calcination system 100 comprises an injector inlet, configured to receive preheated input material, for example lime mud, from a input material preheater 104 into a fluid conductor configured for transferring the preheated input material to an injector.; the injector, being configured to inject the preheated material into an electrically heated calcination reactor 108; and an injection gas 107 supply configured to supply gas for transfer and injection of input material into the electrically heated calcination reactor 108.
  • the injection gas 107 is preheated in an injection gas tube, conducted through the input material preheater 104.
  • the injection gas 107 is supplied in a flow such that smaller particles are lifted by the injection gas stream.
  • This kind of configuration is suitable when the injector is configured to inject the preheated input material into a forma of an electric plasma generator of the electrically heated calcination reactor 108.
  • the injector is configured to inject the preheated input material into a calcination chamber of the electrically heated calcination reactor 108 in an input material stream tangential in relation to a gas plasma stream generated by an electric plasma generator of the electrically heated calcination reactor 108.
  • the injector inlet, and an outlet for the injection gas supply is positioned at an outlet of the input material preheater 104.
  • the electrically heated calcination reactor 108 is thus configured to receive a flow of pre-heated material, such as lime mud, from the injector arrangement and expose the material to heat generated by electricity.
  • Embodiments of the calcination system comprises a the electrically heated calcination reactor 108 being configured to convert input material received by means of the injection arrangement 106 into calcination process products comprising a solid compound, for example in the form of calcium oxide, and a gas, for example in the form of carbon dioxide.
  • Embodiments of a calcination method comprise converting, in the electrically heated calcination reactor 108, input material into calcination process products comprising a solid compound, for example in the form of calcium oxide, and a gas, for example in the form of carbon dioxide.
  • the calcination reactor is electrically heated by an electric gas plasma generator configured to inject hot gas plasma, such as carbon dioxide plasma, into a calcination chamber of the calcination reactor 108, and possibly maintain production of gas plasma in the calcination chamber from gas, such as carbon dioxide CO2, formed in the calcination process.
  • gas plasma such as carbon dioxide plasma
  • the lime mud that is exposed to the heat of the gas plasma is converted to calcination process products in the form of calcium oxide, also called quick lime, and carbon dioxide CO2.
  • the calcination reactor 108 is further configured to exit the heat-treated material and if applicable calcination process products, such as quick lime and carbon dioxide, to a first (1 st ) separator 112.
  • An electric gas plasma generator (not shown in FIG 1 ), comprised in embodiments of the calcination reactor, is devised to supply energy via an electric arc formed between electrodes. Gas is ionized and an energetic gas plasma is formed. Such gas plasma normally has a temperature in the range of 0-4000 degrees Celsius or more at the discharge of the gas plasma generator.
  • the gas plasma generator comprises a nozzle called forma configured to inject gas plasma into the calcination reactor 108. Pressurized gas may be supplied to the forma to overcome a pressure drop occurring over the gas plasma generator. The pressurized gas may be used to control the temperature of the gas plasma.
  • Preheated input material is in the calcination reactor mixed with or exposed to hot gas from the plasma generator.
  • the calcination reactor is in embodiments configured to balance the exposure of the pre-heated input material to heat at too high temperature. For example, for input material comprising lime with calcium carbonate exposure to calcination temperatures exceeding 1. degrees Celsius may entail risk for inactivating the lime, also called dead burning of the lime. Configuring the calcination reactor such that the input material when injected in the calcination reactor is in powder form thus having a large surface and such that the powder formed input material is exposed to heat for a limited period of time enables that inactivation of the input lime is avoided.
  • the input material is calcinated during fragments of seconds to a few seconds. Calcination is preferably carried out at atmospheric pressure, or at a small over-pressure or under-pressure.
  • the calcination reactor 108 may be electrically heated using resistive technology, microwave or radio wave technology, or other electrically driven heating.
  • the first (1 st ) separator 112 is configured to separate resulting process products generated by the heat treatment of the material in the calcination reactor 108, such as solid calcination process products in the form of calcium oxide (quick lime) and gas formed calcination process products in the form of carbon dioxide CO2 when applied in a lime recovery cycle.
  • the temperature of the calcination process products received from the calcination reactor 108 is in lime calcination embodiments exceeding 900 degrees Celsius.
  • larger and/or heavier particles in the material flow input from the calcination reactor 108 are separated from smaller and/or lighter particles and gas.
  • the larger and/or heavier particles are collected in a collection hopper (not shown in FIG 1 ), and residual calcination process products in the form of gas usually together with a certain amount of smaller and/or lighter particles are conducted out from the first separator 112 to a first (1 st ) heat recovery arrangement 116.
  • the first separator 112 is a cyclone, an electric filter or a sedimentation device or sedimentation arrangement.
  • Embodiments of the calcination system 100 comprises one or more separators 112,118 configured to separate the solid compound in the form of calcium oxide and gas in the form of carbon dioxide of the calcination process products.
  • Embodiments of a calcination method comprises separating, in one or more separators 112, 118 the solid compound, for example in the form of calcium oxide and gas, for example in the form of carbon dioxide of the calcination process products.
  • Embodiments of the calcination system 100 comprises: a first separator 112 configured to receive calcination process products from the electrically heated calcination reactor 108 and to separate solid compound, for example in the form of calcium oxide, from the gas, for example in the form of carbon dioxide, of the calcination process products.
  • Embodiments of the calcination method comprise separating, in a first separator 112, calcination process products received from the electrically heated calcination reactor (108) such that solid compound, for example in the form of calcium oxide, is separated from the gas, for example in the form of carbon dioxide, of the calcination process products.
  • the residual calcination process products output from the first separator 112 will comprise and usually mainly consist of carbon dioxide CO2 and fine-grained residual calcium oxide (quick lime).
  • a separation ratio in a cyclone variant of the first separator 112 would for example be in the range of 75 % of the calcium oxide (quick lime) input from the calcination reactor 108 being collected in the collection hopper and in the range of 25 % of the calcium oxide (quick lime) being output from the separator 112 together with carbon dioxide CO2.
  • the first (1 st ) heat recovery arrangement 116 is configured to recover heat from the residual calcination process products output from the first separator 112.
  • Embodiments of the calcination system comprises a first heat recovery arrangement 116 configured to receive the calcination process products, to extract heat from the calcination process products and transfer the extracted heat to the input material in the input material preheater 104.
  • Embodiments of a calcination method comprise extracting, in a first recovery arrangement 116, heat from the calcination process products and transferring the extracted heat to the input material in the input material preheater 104.
  • the first (1 st ) heat recovery arrangement 116 comprises a flow line configured to conduct a flow of residual calcination process products at a first higher temperature into the input material preheater 104, through the input material preheater 104 where residual calcination process products transfer heat to input material moving through the input material preheater 104 and out of the input material preheater 104 at a second lower temperature.
  • the (1 st ) heat recovery arrangement 116 alternatively or additionally comprises a heat pump (not shown in FIG 1 ) configured to extract heat from the residual calcination process products and preferably to transfer the extracted heat to the input material preheater.
  • Embodiments of a calcination system 100 comprises: an input 102 for receiving input material, for example in the form of lime mud; a input material preheater 104 coupled to the input and configured to conduct input material in a plurality of channels; an injection arrangement 106 configured to receive input material from the input material preheater 104 and to inject input material into an electrically heated calcination reactor 108; a the electrically heated calcination reactor 108 being configured to convert input material received by means of the injection arrangement 106 into calcination process products comprising a solid compound in the form of calcium oxide and a gas in the form of carbon dioxide; a first heat recovery arrangement 116 configured to receive the calcination process products, to extract heat from the calcination process products and transfer the extracted heat to the input material in the input material preheater 104; and one or more separators 112, 118 configured to separate the solid compound in the form of calcium oxide and gas in the form of carbon dioxide of the calcination process products.
  • Embodiments of a calcination method comprising: receiving input material, for example in the form of lime mud; conducting the input material in a plurality of channels of a input material preheater 104; injecting input material into an electrically heated calcination reactor 108; converting, in the electrically heated calcination reactor 108, input material into calcination process products comprising a solid compound in the form of calcium oxide and a gas in the form of carbon dioxide; extracting, in a first recovery arrangement 116, heat from the calcination process products and transferring the extracted heat to the input material in the input material preheater 104; and separating, in one or more separators 112, 118, the solid compound in the form of calcium oxide and gas in the form of carbon dioxide of the calcination process products.
  • Embodiments of a second (2 nd ) heat recovery arrangement 114 are shown in FIG 4.
  • a second (2 nd ) heat recovery arrangement 114 comprised in certain embodiments, is arranged to extract heat from the first separator 112. Such extracted heat is carried in a gas, and the thus heated gas may be used as input into the injection arrangement 106.
  • the second (2 nd ) heat recovery arrangement 114, the flow of extracted heat and the flow lines for the heated gas are in the figures drawn with intermittent lines as to indicate optional features.
  • the heated gas from the second heat recovery arrangement 114 may be used as input to the injection arrangement 106 and/or into the calcination reactor 108.
  • the heated gas may be used as input in or at the forma where it on one hand cools the gas plasma, and on the other hand also contributes with useful heat energy.
  • the second heat recovery arrangement 114 is controllable by one or more actuators, preferably coupled to the control unit 124, with regard to one or more parameters such as flow, amount of energy, temperatures and pressure.
  • Embodiments of the calcination system 100 comprises: a second heat recovery arrangement 114 configured to extract heat from solid compound, for example in the form of calcium oxide, of the calcination process products output from the electrically heated calcination reactor 108 and separated from the gas, for example in the form of carbon dioxide, of the calcination process products, the extracted heat being carried by a gas and inserted into the injection arrangement 106.
  • a second heat recovery arrangement 114 configured to extract heat from solid compound, for example in the form of calcium oxide, of the calcination process products output from the electrically heated calcination reactor 108 and separated from the gas, for example in the form of carbon dioxide, of the calcination process products, the extracted heat being carried by a gas and inserted into the injection arrangement 106.
  • Embodiments of the calcination method comprise extracting, in a second heat recovery arrangement 114, heat from solid compound, for example in the form of calcium oxide, of the calcination process products output from the electrically heated calcination reactor 108 and separated from the gas, for example in the form of carbon dioxide, of the calcination process products, carrying the extracted heat by a gas and inserting the heat carrying gas into the injection arrangement 106.
  • Embodiments of the heat recovery arrangement 114 comprises an inlet for receiving incoming gas from the system 100 for calcination of lime mud.
  • the incoming gas is preheated by excess heat generated by the system 100 for calcination of lime mud.
  • the heat recovery arrangement 114 further comprises an expander 404 for expanding and cooling the incoming preheated gas, and a heat recovery tube 406 arranged in a container 408 comprising quick lime extracted from the system (100) for calcination of lime mud.
  • the heat recovery tube 406 may be arranged in any container in the system 100 comprising heated material.
  • the expanded and cooled gas is led into the tube 410 and is heated by the heat from the quick lime in the container.
  • the heat recovery arrangement 114 further comprises a compressor 412 for compressing and further heating the heated gas and an outlet 414, for example comprising a diffusor for alleviating the downstream tubes from excessive pressure, from which the compressed and further heated gas is led out and reentered into the system 100 for calcination of lime mud, whereby heat generated from the calcination process is reused.
  • the compressed and further heated gas received from the heat recovery arrangement 114 may have a temperature of about 1000 - 1 degrees Celcius, and may be reentered into different parts of the system 100, for example into the injection arrangement 106, or into the input material preheater 104, or directly into the calcination reactor 108.
  • a steam boiler 120 is configured to extract remaining heat from the residual calcination process products received from the first heat recovery arrangement and before residual solid compounds is separated from gas in a subsequent second separator 118.
  • the solid compound is calcium oxide and gas is carbon dioxide CO2.
  • Steam generated in the steam boiler 120 is conducted from the steam boiler 120, for example for use to support processes in embodiments of the calcination system or for use in other processes in a facility employing embodiments of the calcination system.
  • pressurized steam is generated producing process steam or power. Power may be produced in power generators for example in the form of a turbine.
  • the temperature of the residual calcination process products entering the steam boiled is for example in lime calcination embodiments usually in the range of 400-500 degrees Celsius, whereas after having passed the steam boiler 120, the temperature of the residual calcination process products may be for example be in the range of. degrees Celsius.
  • Embodiments of the calcination system comprises a steam boiler 120 configured to extract heat from calcination process products from the preceding heat recovery arrangement and to generate steam.
  • Embodiments of the calcination method comprise extracting, in a steam boiler 120, heat from gas of calcination process products from the one or more separators and generating steam.
  • the residual calcination process products having passed the 1 st heat recovery arrangement 116 is conducted to a second (2 nd ) separator 118 configured to separate residual calcination process products. For example, remaining solid compounds is separated from gas.
  • the second (2 nd ) separator 118 is a cyclone.
  • residual calcium oxide is further separated from carbon dioxide CO2.
  • Solid compounds, such as calcium oxide in lime calcination embodiments, is collected in a collection hopper and the further cleaned gas, such as carbon dioxide CO2, is conducted to a filter arrangement 122 via an optional steam boiler 120.
  • Embodiments of the calcination system 100 comprises: a second separator 118 configured to receive residual calcination process products output from the first separator 112 and from the first heat recovery system 116, the second separator 118 being configured to further separate solid compound, for example in the form of calcium oxide, from the gas, for example in the form of carbon dioxide, of the residual calcination process products.
  • Embodiments of the calcination method comprise separating, in a second separator 118, residual calcination process products received from the first separator 112 and from the first heat recovery system 116, such that further solid compound, for example in the form of calcium oxide, is separated from the gas, for example in the form of carbon dioxide, of the residual calcination process products.
  • the filter arrangement 122 is configured to filter the gas component of the calcination process products to a higher degree of purity before collecting, storing and/or using the output gas.
  • the gas component of the calcination process products is carbon dioxide CO2.
  • the filter arrangement 122 would comprise a filter adapted to filter carbon dioxide CO2.
  • the filtered gas component of the calcination process products is conducted to a gas output 124.
  • textile filters may be applied.
  • the filter arrangement 122 is in embodiments configured to filter out possible dust and such impurities still present in the gas output from the second separator 118.
  • Embodiments of the calcination system comprises a filter arrangement 122 configured to receive gas of calcination process products, for example in the form of carbon dioxide, from the one or more separators and to filter the gas to a higher degree of purity.
  • Embodiments of the calcination method comprises filtering, in a filter arrangement 122 gas of calcination process products, for example in the form of carbon dioxide, received from the one or more separators, such that the gas is filtered to a higher degree of purity.
  • the gas output 124 is configured to receive the gas component of the calcination process products, and is in different embodiments configured to store, temporarily or for a longer term, or conduct the gas to the calcination system itself or to other systems and/or processes.
  • the gas conducted to the gas output 124 would be carbon dioxide CO2, and would in embodiments be recirculated to the calcination reactor.
  • a control unit 126 comprised in embodiments, is configured to receive sensor signals, to generate control signals and to communicate control signals through a control port 128 connected to one or more signal lines 130.
  • the one or more signal lines is schematically indicated as an intermittent line that is connected to sensors and/or control actuators (not shown) at different points and components of the calcination system in order to control various parameters.
  • Embodiments of the calcination system 100 comprising a control unit 126 communicatively coupled to sensors and control actuators and configured to receive sensor signals, to generate control signals and to communicate control signals through a control port 128 connected to one or more signal lines 130 coupled to the sensors and control actuators.
  • Embodiments of the calcination method comprises in a control unit 126 communicatively coupled to sensors and control actuators, receiving sensor signals, generating control signals and communicating control signals through a control port 128 connected to one or more signal lines 130 coupled to the sensors and control actuators.
  • control unit is configured to control one or more of: driving gas supply 105 into the input material preheater 104; injection gas supply 107 into the injection arrangement 106; heated gas in the particle separator 110; gas pressure in the calcination chamber 108; and/or temperature in the calcination chamber 108.
  • Embodiments of the calcination method further comprises controlling one or more of: driving gas supply 105 into the input material preheater 104; injection gas supply (107) into the injection arrangement 106; heated gas in the particle separator 110; gas pressure in the calcination chamber 108; and/or temperature in the calcination chamber 108.
  • the heat recovery arrangement 114 comprises an inlet for receiving incoming gas from the system 100 for calcination of lime mud.
  • the incoming gas is preheated by excess heat generated by the system 100 for calcination of lime mud.
  • the heat recovery arrangement 114 may further comprise an expander 404 for expanding and cooling the incoming preheated gas and a heat recovery tube 406 arranged in a container 408 comprising quick lime extracted from the system 100 for calcination of lime mud.
  • the expanded and cooled gas is led into the recovery tube 410 and is heated by the heat from the quick lime.
  • the heat recovery arrangement 114 may further comprise a compressor 412 for compressing and further heating the preheated gas and an outlet 414 from which the compressed and further heated gas is led out and reentered into the system 100 for calcination of lime mud. Thereby heat generated from the calcination process is reused.
  • the incoming gas may be carbon dioxide CO2 with a temperature of approximately, degrees and a pressure of approximately 4 bar (a).
  • the outcoming gas may have a temperature of approximately 1000 - 1 degrees and a pressure of approximately 2 bar (a).
  • the heat recovery arrangement 114 comprise a diffuser 418 arranged to diffuse the outcoming gas from the outlet 414. Thanks to the diffuser, the gas is presented with a lower pressure but high temperature which provides for a more safe solution.
  • the compressor 412 may be arranged inside a housing 420. The housing 420 protects adjacent equipment from dangerous hot gas with high pressure.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Ceramic Engineering (AREA)
  • Materials Engineering (AREA)
  • Structural Engineering (AREA)
  • Compounds Of Alkaline-Earth Elements, Aluminum Or Rare-Earth Metals (AREA)

Abstract

Des modes de réalisation de la présente invention concernent un séparateur de particules (110) destiné à être utilisé dans un système de calcination (100). Le système de calcination (100) comprend un réacteur de calcination chauffé électriquement (108) configuré pour convertir un matériau d'entrée en produits du procédé de calcination. Le séparateur de particules (110) comprend une chambre (401) conçue pour contenir un lit fluidisé (402) de particules mélangées à du gaz, dans lequel du gaz à lit fluidisé (402) est évacué par le dessous (403), ce qui permet de séparer des particules plus petites de particules plus grandes en soulevant lesdites particules plus petites vers le haut dans le flux de gaz. Le lit fluidisé (402) est couplé à un canal de transfert (404) agencé pour fournir l'écoulement des particules plus petites séparées mélangées avec du gaz à un agencement d'injection (106) injectant le matériau d'entrée fourni dans ledit réacteur de calcination chauffé électriquement (108).
PCT/SE2024/050193 2023-03-01 2024-02-29 Séparateur de particules, système comprenant un tel séparateur de particules, et procédés de calcination Pending WO2024181909A1 (fr)

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
SE2350232A SE545972C2 (en) 2023-03-01 2023-03-01 A calcination method and system comprising a particle separator
SE2350232-1 2023-03-01
SE2350231-3 2023-03-01
SE2350231A SE547412C2 (en) 2023-03-01 2023-03-01 Particle separator in a calcination system and a method for supplying material to a calcination process

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Citations (9)

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US3630504A (en) * 1970-01-05 1971-12-28 Dow Chemical Co Method of calcination and hydration and unit therefor
FR2321674A1 (fr) * 1975-08-20 1977-03-18 Lambert Ind Moyen d'echange de chaleur utilisable notamment dans les traitements des pulpes de matieres granuleuses, pulverulentes ou colloidales
US5378319A (en) * 1993-05-07 1995-01-03 Tran Industrial Research Inc. Lime mud calcining using dielectric hysteresis heating
US5919038A (en) * 1996-02-29 1999-07-06 Fuller Company Method for the calcination of calcium carbonate bearing materials
WO2002096821A1 (fr) * 2001-05-30 2002-12-05 Vattenfall Ab Procede et dispositif de calcination
EP1580511A2 (fr) * 2004-03-24 2005-09-28 Coperion Waeschle GmbH & Co. KG Dispositif pour maintenir la température de matière en vrac
US20150056125A1 (en) * 2006-08-25 2015-02-26 Robert A. Rossi Process and system for producing commercial quality carbon dioxide from recausticizing process calcium carbonates
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Publication number Priority date Publication date Assignee Title
US3630504A (en) * 1970-01-05 1971-12-28 Dow Chemical Co Method of calcination and hydration and unit therefor
FR2321674A1 (fr) * 1975-08-20 1977-03-18 Lambert Ind Moyen d'echange de chaleur utilisable notamment dans les traitements des pulpes de matieres granuleuses, pulverulentes ou colloidales
US5378319A (en) * 1993-05-07 1995-01-03 Tran Industrial Research Inc. Lime mud calcining using dielectric hysteresis heating
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WO2002096821A1 (fr) * 2001-05-30 2002-12-05 Vattenfall Ab Procede et dispositif de calcination
EP1580511A2 (fr) * 2004-03-24 2005-09-28 Coperion Waeschle GmbH & Co. KG Dispositif pour maintenir la température de matière en vrac
US20150056125A1 (en) * 2006-08-25 2015-02-26 Robert A. Rossi Process and system for producing commercial quality carbon dioxide from recausticizing process calcium carbonates
US20200108346A1 (en) * 2018-10-05 2020-04-09 8 Rivers Capital, Llc Direct gas capture systems and methods of use thereof
US20200361819A1 (en) * 2019-05-13 2020-11-19 Carmeuse North America Calciner using recirculated gases

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